Apparatus and process for converting aromatic compounds by benzene alkylation with ethanol

ABSTRACT

Apparatus and process for converting aromatic compounds, comprising/using: a fractionating train (4-7) suitable for extracting at least one benzene-comprising fraction (22), one toluene-comprising fraction (23) and one fraction (24) comprising xylenes and ethylbenzene from the feedstock (2); a xylene separating unit (10) suitable for treating the fraction comprising xylenes and ethylbenzene and producing a para-xylene-comprising extract (39) and a raffinate (40) comprising ortho-xylene, meta-xylene and ethylbenzene; an isomerizing unit (11) for treating the raffinate and producing a para-xylene-enriched isomerizate (42), which is sent to the fractionated train; and an alkylating reaction section (13) for treating at least part of the benzene-comprising fraction with an ethanol source (30) and producing an alkylation effluent (31) comprising ethylbenzene, which is sent to the isomerizing unit.

TECHNICAL FIELD

The invention pertains to the conversion of aromatics in the context ofthe production of aromatics for petrochemicals (benzene, toluene,para-xylene, ortho-xylene). The object of the invention moreparticularly is to be able to control the respective amounts of benzeneand para-xylene, and in particular to be able to produce onlypara-xylene.

The aromatic complex (or apparatus for converting aromatic compounds) issupplied with feedstocks composed predominantly of six to ten carbonatoms or more, referred to as C6 to 010+ feedstocks. Various sources ofaromatic compounds may be introduced into an aromatic complex, the mostwidespread of such source being the process in which naphthas aresubjected to catalytic reforming. Mixtures of aromatic compoundsobtained from a process of converting lignocellulosic biomass may alsobe introduced, after a purification treatment, into an aromatic complex.The process of catalytic pyrolysis of lignocellulosic biomass, forexample, may be considered as a source of aromatics.

Within an aromatic complex, irrespective of the source of aromatics,benzene and alkylaromatics (e.g. toluene, para-xylene, ortho-xylene) areextracted therefrom and then converted into desired intermediates. Theproducts of interest are aromatics having 0 (benzene), 1 (toluene) or 2(xylenes) methyl groups, and more particularly, among the xylenes,para-xylene, which has the greatest market value.

It is therefore appropriate to dispose methyl groups in such a way thatall of the aromatic ring systems exiting the aromatic complex possesstwo methyl groups (e.g. para-xylene, ortho-xylene)

PRIOR ART

To date, aromatic complexes make it possible to produce benzene,optionally toluene, and xylenes (often para-xylene, sometimesortho-xylene). An aromatic complex generally possesses at least onecatalytic unit having at least one of the following functions:

-   -   isomerizing aromatic compounds having eight carbon atoms        referred to as A8 compounds, which allows ortho-xylene,        meta-xylene and ethylbenzene to be converted into para-xylene;    -   transalkylation, which allows xylenes to be produced from a        mixture of toluene (and optionally of benzene) and of A9+        compounds such as trimethylbenzenes and tetramethylbenzenes; and    -   disproportionation of the toluene, which allows the production        of benzene and of xylenes.

The aromatic group allows production of high-purity para-xylene viaseparation by adsorption or by crystallization, an operation which iswell known in the prior art. This “C8 aromatic loop” includes a step ofremoving the heavy compounds (i.e., C9+) in a distillation column whichis called the “xylenes column”. The overhead flow from this column,which contains the C8 aromatic isomers (i.e., A8), is then sent into thepara-xylene separation process, which is, very generally, a process forseparation by simulated moving bed (SMB) adsorption, to produce anextract and a raffinate, or a crystallization process, in which apara-xylene fraction is isolated from the rest of the constituents ofthe mixture in the form of crystals.

The extract, which contains the para-xylene, is then distilled to givethe high-purity para-xylene. The raffinate, which is rich inmeta-xylene, ortho-xylene and ethylbenzene, is treated in a catalyticisomerizing unit, which returns a mixture of C8 aromatics in which theproportion of xylenes (ortho-, meta-, para-xylenes) is virtually atthermodynamic equilibrium and the amount of ethylbenzene is reduced.This mixture is again sent into the “xylenes column” with the freshfeedstock.

All of the industrial processes for isomerizing C8 aromatics enable theisomerization of xylenes. The conversion of the ethylbenzene, on theother hand, is dependent on the type of process and of catalyst that areselected. The reason is that petrochemical complexes utilize either an“isomerizing” isomerizing unit (i.e. isomerization of ethylbenzene intoa mixture of C8 aromatics) or a “dealkylating” isomerizing unit (i.e.,dealkylation of ethylbenzene into benzene), in order to promote theproduction (at the exit from the aromatic loop) respectively either ofpara-xylene alone or of benzene and para-xylene.

The selection of an “isomerizing” isomerization makes it possible, asindicated above, to maximize the production of para-xylene, which is thecompound having the highest added value at the exit from the aromaticcomplex. The combination of an “isomerizing” isomerization and aliquid-phase isomerization within an aromatic complex, as described forexample in U.S. Pat. Nos. 8,697,929, 7,371,913, 4,962,258, 6,180,550,7,915,471, U.S. Ser. No. 10/035,739 and U.S. Ser. No. 10/029,958, makesit possible in particular to maximise the amount of para-xylene producedwhile reducing the loss of aromatic rings, relative to a prior-artaromatic complex.

SUMMARY OF THE INVENTION

In the context described above, a first object of the present inventionis to overcome the problems of the prior art and to provide an apparatusand a process for producing aromatics for petrochemicals that allow therespective amounts of benzene and para-xylene to be adjusted for anytype of feedstock supplied to an aromatic complex, or even of producingonly para-xylene. The subject of the invention also makes it possible toincrease the amounts of aromatics produced, and to retain the bio-basednature of the aromatics when said aromatics have come from alignocellulosic biomass conversion process.

The invention resides in the introduction of ethanol into the aromaticcomplex and in the provision of one or more units which enable theethanol to be converted and, in particular, which enable onlypara-xylene to be produced. Specifically, the subject of the presentinvention may be summarized as the addition of a catalytic unit to thearomatic complex, this catalytic unit enabling benzene to be convertedinto ethylbenzene by reaction of benzene with ethanol. This unitcomprises an alkylated reaction section which produces ethylbenzene. Anoptional transalkylating reaction section may also allow thepolyethylbenzenes, which are possible by-products of the alkylationreaction of benzene with ethanol, to be converted into ethylbenzenes.The ethylbenzene thus produced is converted into para-xylene in thearomatic loop of the aromatic complex.

According to a first aspect, the aforementioned objects, and also otheradvantages, are obtained by an apparatus for converting a feedstock ofaromatic compounds, comprising:

-   -   a fractionating train suitable for extracting at least one        fraction comprising benzene, one fraction comprising toluene and        one fraction comprising xylenes and ethylbenzene from the        feedstock;    -   a xylene separating unit suitable for treating the fraction        comprising xylenes and ethylbenzene and for producing an extract        comprising para-xylene and a raffinate comprising ortho-xylene,        meta-xylene and ethylbenzene;    -   an isomerizing unit suitable for treating the raffinate and        producing a para-xylene-enriched isomerizate, which is sent to        the fractionating train; and    -   an alkylating reaction section suitable for treating at least        part of the benzene-comprising fraction with a source of ethanol        and producing an alkylating effluent comprising ethylbenzene,        which is sent to the isomerizing unit.

According to one or more embodiments, the device further comprises atransalkylating reaction section suitable for transalkylatingpolyethylbenzenes present in the alkylation effluent and producing anethylbenzene-enriched fraction.

According to one or more embodiments, the device further comprises afractionating unit suitable for treating the alkylation effluent andproducing a plurality of fractionation fractions comprising at least oneethylbenzene fraction, which is sent to the isomerizing unit, oneaqueous fraction comprising water, and one benzene fraction.

According to one or more embodiments, the fractionating unit is disposeddownstream of the transalkylated reaction section and is suitable fortreating the ethylbenzene-enriched fraction.

According to one or more embodiments, the fractionating unit is suitablefor producing additionally at least one polyethylbenzene fraction, andthe transalkylating reaction section is disposed downstream of thefractionating unit and is suitable for treating at least part of saidpolyethylbenzene fraction.

According to one or more embodiments, the fractionating train issuitable for extracting a C9-C10 monoaromatics fraction from thefeedstock.

According to one or more embodiments, the device further comprises atransalkylating unit suitable for treating the C9-C10 monoaromaticsfraction with the toluene-comprising fraction and producing xylenes,which are sent to the fractionating train.

According to one or more embodiments, the device further comprises adisproportionating unit suitable for treating at least partly thetoluene-comprising fraction and producing a xylene-enriched fraction,which is recycled to the isomerizing unit.

According to a second aspect, the aforementioned objects, and also otheradvantages, are obtained by a process for converting a feedstock ofaromatic compounds, comprising the following steps:

-   -   fractionating the feedstock in a fractionating train to extract        at least one benzene-comprising fraction, one toluene-comprising        fraction and one fraction comprising xylenes and ethylbenzenes;    -   separating the fraction comprising xylenes and ethylbenzene in a        xylene separating unit and producing a para-xylene-comprising        extract and a raffinate comprising ortho-xylene, meta-xylene and        ethylbenzene;    -   isomerizing the raffinate in an isomerizing unit and producing a        para-xylene-enriched isomerizate;    -   sending the para-xylene-enriched isomerizate to the        fractionating train;    -   alkylating at least part of the benzene-comprising fraction with        an ethanol source in an alkylating reaction section and        producing an alkylation effluent comprising ethylbenzene; and    -   sending the alkylation effluent comprising ethylbenzene to the        isomerizing unit.

According to one or more embodiments, the alkylated reaction sectioncomprises at least one alkylating reactor, which is used under thefollowing operating conditions:

-   -   temperature of between 20° C. and 400° C.;    -   pressure of between 1 and 10 MPa;    -   molar benzene/ethanol ratio of between 3 and 15;    -   WWH of between 0.5 and 50 h⁻¹.

According to one or more embodiments, the alkylated reactor is operatedin the presence of catalysts comprising a zeolite.

According to one or more embodiments, the isomerizing unit comprises agas-phase isomerization zone and/or a liquid-phase isomerization zone,

wherein the gas-phase isomerization zone is used under the followingoperating conditions:

-   -   temperature of greater than 300° C.;    -   pressure of less than 4.0 MPa;    -   hourly space velocity of less than 10 h⁻¹;    -   molar hydrogen-to-hydrocarbon ratio of less than 10;    -   in the presence of a catalyst comprising at least one zeolite        having channels whose opening is defined by a ring of 10 or 12        oxygen atoms, and at least one group VIII metal in an amount of        between 0.1 and 0.3 weight %, endpoints included, and        wherein the liquid-phase isomerization zone is used under the        following operating conditions:    -   temperature of less than 300 C;    -   pressure of less than 4 MPa;    -   hourly space velocity of less than 10 h⁻¹;    -   in the presence of a catalyst comprising at least one zeolite        having channels whose opening is defined by a ring of 10 or 12        oxygen atoms.

According to one or more embodiments, the process further comprises thefollowing step:

-   -   transalkylating polyethylbenzenes present in the alkylation        effluent in a transalkylating reaction section and producing an        ethylbenzene-enriched fraction, and    -   sending the ethylbenzene-enriched fraction to the isomerizing        unit.

According to one or more embodiments, the transalkylating reactionsection comprises at least one transalkylation reactor, which is usedunder the following operating conditions:

-   -   temperature of between 200° C. and 400° C.;    -   pressure of between 1 and 6 MPa;    -   WWH of between 0.5 and 5 h⁻¹.

According to one or more embodiments, the transalkylation reactor isoperated in the presence of a catalyst comprising a zeolite.

Embodiments according to the first aspect and the second aspect, andalso other characteristics and advantages of the apparatuses andprocesses according to the abovementioned aspects, will become apparenton reading the description which follows, which is given solely by wayof illustration and without limitation, and with reference to thedrawings which follow.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows a schematic view of a process according to the presentinvention, enabling an increase in the production of para-xylene.

FIG. 2 shows a schematic view of a process according to the presentinvention, enabling an increase in the production of para-xylene, inwhich the transalkylating unit is replaced with a disproportionatingunit, and in which the transalkylating reaction section is disposeddownstream of the fractionating unit.

DESCRIPTION OF THE EMBODIMENTS

Embodiments of the device according to the first aspect and of theprocess according to the second aspect will now be described in detail.In the detailed description below, numerous specific details are set outin order to convey a deeper understanding of the apparatus. However, itwill be apparent to the skilled person that the apparatus can beemployed without these specific details. In other cases, characteristicswhich are well known have not been described in detail, in order not tocomplicate the description to no purpose.

In the present specification, the term “comprise” is synonymous with(signifies the same thing as) “include” and “contain”, and is inclusiveor open, and does not exclude other elements which are not stated. It isunderstood that the term “comprise” includes the exclusive and closedterm “consist”. Moreover, in the present description, an effluentcomprising essentially or solely compounds A corresponds to an effluentcomprising at least 80 or 90 weight %, preferably at least 95 weight %,very preferably at least 99 weight % of compounds A.

The present invention may be defined as an apparatus and a processcomprising a sequence of unitary operations which enable the productioneither of para-xylene exclusively or of para-xylene and benzene.

The apparatus and the process according to the invention arecharacterized in that in that they comprise and use the catalytic unitsand the separating units that are known to the skilled person forproducing benzene and para-xylene, these units being commonlyencountered in aromatic complexes, and in that they comprise and use areaction section for alkylating benzene using ethanol, and optionally areaction section for transalkylating polyethylbenzene by-products. Saidreaction section for alkylating benzene with ethanol producesethylbenzene. One of the characteristics of the present invention is theselective conversion of this ethylbenzene, obtained by alkylation,within a unit for isomerizing aromatic C8 compounds, said isomerizingunit treating aromatic compounds of the aromatic complex with theaddition of the ethylbenzene produced by alkylating benzene withethanol.

Surprisingly, the combination of the reaction section for alkylatingbenzene with ethanol, and of the isomerizing unit, enables not only anincrease in the amount of aromatics produced but also the possibility ofobtaining only para-xylene, and the preservation of the bio-basedcharacter of the para-xylene, in the case where the source of aromaticcompounds entering the aromatic complex has come from a lignocellulosicbiomass conversion process, such as, for example, a process of catalyticpyrolysis of biomass, and in the case where the ethanol is alsobio-based.

Referring to FIG. 1, according to one or more embodiments, the apparatusfor converting the aromatic compounds comprises:

-   -   an optional feedstock separating unit 1 for separating the        entering feedstock 2 for the aromatic complex into a 7 carbon        atoms or fewer (C7−) hydrocarbon fraction and an 8 carbon atoms        or more (A8+) aromatic fraction;    -   an optional aromatics extraction unit 3 between the feedstock        separating unit 1 and a fractionated train 4-7, for separating        the aliphatic compounds from the benzene and the toluene in the        C7− fraction of the feedstock for the complex;    -   the fractionating train 4-7 downstream of the optional aromatics        extraction unit 3, enabling the extraction of the benzene, the        toluene and the xylenes from the other aromatics;    -   an optional transalkylating unit 8, which converts the toluene        (and optionally the benzene) and methylalkylbenzenes such a        trimethylbenzenes into xylenes—advantageously this unit may also        treat tetramethylbenzenes;    -   an optional selective hydrogenolysis unit 9 suitable for        treating a fraction comprising aromatic compounds having 9 and        10 carbon atoms, and producing a hydrogenolysis effluent which        is enriched in methyl-substituted aromatic compounds;    -   an optional separating unit (not shown) for separating the        hydrogenolysis effluent disposed (e.g., directly) downstream of        the selective hydrogenolysis unit 9, for producing a plurality        of liquid effluent fractions;    -   a xylene separating unit 10 (e.g., a crystallization unit or        simulated moving bed unit employing a molecular sieve and a        desorbent such as toluene), which enables the para-xylene to be        isolated from the xylenes and the ethylbenzene;    -   a unit 11 for isomerizing the raffinate obtained as effluent        from the xylene separating unit 10, for conversion in particular        of the ortho-xylene, meta-xylene and ethylbenzene into        para-xylene;    -   an optional stabilizing column 12, which enables in particular        the withdrawal of the more volatile species (e.g., C5−) from the        aromatic complex, especially the effluents from the        transalkylating unit 8 and/or the isomerizing unit 11;    -   an alkylating reaction section 13 for alkylating a        benzene-comprising fraction with ethanol and producing        ethylbenzene;    -   an optional transalkylating section 14, for transalkylating the        polyethylbenzenes obtained from the alkylating reaction section        13 and producing an ethylbenzene-enriched effluent;    -   a fractionating unit 15 for separating the alkylation products,        disposed downstream of the alkylating reaction section 13.

Advantageously, the alkylating reaction section 13 enables theproduction of a surplus of aromatics by the addition of ethanol (addingtwo carbon atoms to each molecule of benzene), and provides thepossibility of being able to convert the entirety of the benzene intopara-xylene. Furthermore, the small amount of heavy compounds obtainedfrom the section of alkylating benzene with ethanol, this amount notbeing used for transalkylation with the benzene, may be utilized as fuel(e.g., kerosene or gas-oil).

Referring to FIG. 1, the feedstock separating unit 1 treats thefeedstock 2 entering the aromatic complex, to separate an overheadfraction 16 comprising (e.g., essentially) compounds having 7 carbonatoms or fewer (C7−), containing, in particular benzene and toluene, anda bottom fraction 17 comprising (e.g., essentially) aromatics having 8carbon atoms or more (A8+), which is sent to the xylene column 6.According to one or more embodiments, the feedstock separating unit 1also separates a first toluene fraction 18 comprising at least 90 weight%, preferably at least 95 weight %, very preferably at least 99 weight %of toluene. According to one or more embodiments, the first toluenefraction 18 is sent to the first column 4 for distilling aromaticcompounds, also referred to as the benzene column, and/or to the secondcolumn 5 for distilling aromatic compounds, also referred to as thetoluene column.

According to one or more embodiments, the entering feedstock 2 is ahydrocarbon fraction containing predominantly (i.e., >50 weight %)molecules whose carbon number is from 6 to 10 carbon atoms. Thisfeedstock may also contain molecules having more than 10 carbon atomsand/or molecules having 5 carbon atoms.

The feedstock 2 entering the aromatic complex is rich in aromatics(e.g. >50 weight %) and contains preferably at least 20 weight % ofbenzene, more preferably at least 30 weight %, very preferably at least40 weight % of benzene. The entering feedstock 2 may be produced bycatalytic reforming of a naphtha, or may be a product of a cracking unit(e.g., steam cracking, catalytic cracking), or of any other means forproducing alkylaromatics.

According to one or more embodiments, the entering feedstock 2 isbio-based. According to one or more embodiments, the entering feedstock2 originates from a lignocellulosic biomass conversion process. Forexample, an effluent produced by conversion of lignocellulosic biomassmay be treated to meet the required specifications of the enteringfeedstock 2 as described above, so as to have contents of sulfur,nitrogen and oxygen elements that are compatible with an aromaticcomplex. According to one or more embodiments, the entering feedstock 2comprises less than 10 ppm by weight, preferably less than 5 ppm byweight, very preferably less than 1 ppm by weight of elemental nitrogen,and/or less than 10 ppm by weight, preferably less than 5 ppm by weight,very preferably less than 1 ppm by weight of elemental sulfur, and/orless than 100 ppm by weight, preferably less than 50 ppm, verypreferably less than 10 ppm by weight of elemental oxygen.

The overhead fraction 16 from the feedstock separating unit 1,optionally mixed with the bottom product (benzene and toluene) from thestabilizing column 12, which will be defined hereinafter, is sent to thearomatics extraction unit 3 for the extraction of an effluent 19comprising C6-C7 19 aliphatic species, which is exported as a co-productof the aromatic complex. The fraction called aromatic fraction 20(essentially benzene and toluene) which is extracted from the aromaticsextraction unit 3, optionally mixed with the heavy fraction 21 from thetransalkylating unit 8, which will be defined hereinafter, is sent tothe benzene column 4. According to one or more embodiments, the aromaticfraction 20 is a C6-C7 aromatic (A6-A7) hydrocarbon (e.g., essentially)feedstock.

According to one or more embodiments, the fractionated train comprisesthe columns 4, 5, 6 and 7 for distilling aromatic compounds, enablingthe separation of the following five fractions:

-   -   a fraction 22 comprising (e.g., essentially) benzene;    -   a fraction 23 comprising (e.g., essentially) toluene;    -   a fraction 24 comprising (e.g., essentially) xylenes and        ethylbenzene;    -   a fraction 25 comprising (e.g., essentially) aromatic compounds        having 9 and 10 carbon atoms;    -   a fraction 26 comprising (e.g., essentially) aromatic compounds,        in which the most volatile species are aromatics having 10        carbon atoms.

The benzene column 4 is suitable for: treating the aromatic fraction 20,which is a C6-010 (e.g., essentially) aromatic hydrocarbon feedstock(A6+); producing at the top the benzene-comprising fraction 22, whichmay be one of the desired products exiting the aromatic complex; andproducing at the bottom a C7-010 (e.g., essentially) aromatic effluent27 (A7+).

The toluene column 5 is suitable for: treating the C7-010 aromaticeffluent 27 (A7+), the bottom product from the benzene column 4;producing at the top the toluene-comprising fraction 23, which is passedto the transalkylating unit 8; and producing at the bottom a C8-010(e.g., essentially) aromatic effluent 28 (A8+).

The third distillation column, 6, for aromatic compounds, also referredto as the xylene column, is suitable for: treating the aromatic fraction17 having 8 or more carbon atoms (A8+) of the feedstock of the aromaticcomplex and optionally the bottom effluent 28 from the toluene column;producing at the top the fraction 24 comprising xylenes andethylbenzene, which is passed to the xylenes separating unit 10; andproducing at the bottom an effluent 29 (e.g., essentially) comprisingC9-010 aromatics (A9+).

The fourth distillation column, 7, for aromatic compounds, also referredto as the heavy aromatics column, is optional and is suitable for:treating the bottom effluent 29 from the xylene column; producing at thetop the fraction 25 comprising C9-C10 monoaromatics; and producing atthe bottom the fraction 26 comprising (e.g., essentially) aromaticcompounds of which the more volatile species are aromatics having 10carbon atoms (A10+). The bottom fraction 26 preferably comprises 011+compounds.

Obtained at the top of the benzene column 4 is the benzene-comprisingfraction 22, which is sent at least partly to the alkylating reactionsection 13 for reaction with an ethanol source 30 to produce analkylation effluent 31 comprising ethylbenzene, water, and potentiallybenzene and/or ethanol and/or polyethylbenzenes (by-products) and/oroligomers formed from the ethanol. According to one or more embodiments,the alkylating reaction section 13 is fed with a mixture consisting(e.g., essentially) of benzene and of ethanol (and optionally of water).

According to one or more embodiments, the alkylation effluent 31comprises at least 5 weight %, preferably at least 8 weight %, verypreferably at least 10 weight % of ethylbenzene. The balance to 100 iscomposed primarily (e.g. >50 weight %), or even essentially, of benzene,the latter being generally used in excess.

According to one or more embodiments, the alkylating reaction section 13comprises at least one alkylation reactor suitable for use under atleast one of the following operating conditions:

-   -   temperature of between 20° C. and 400° C., preferably between        150° C. and 400° C., and more preferably still of between        250° C. and 310° C.;    -   pressure of between 1 and 10 MPa, preferably of between 2 and 7        MPa, and more preferably of between 3 and 5 MPa;    -   molar benzene/ethanol ratio of between 3 and 15, and preferably        between 5 and 12;    -   WWH of between 0.5 and 50 h⁻¹, preferably of between 1 and 10        h⁻¹, and more preferably of between 1.5 and 3 h⁻¹.

The term WWH corresponds to the hourly weight of hydrocarbon feedstockinjected, based on the weight of catalyst charged.

According to one or more embodiments, the alkylating reactor is operatedin the presence of a catalyst comprising a zeolite. According to one ormore embodiments, the zeolite-based catalyst, based preferably onzeolite Y and very preferably on dealuminated zeolite Y, comprises from1 to 100 weight %, preferably 20 to 98 weight %, for example 40 to 98weight % of said zeolite and 0 to 99 weight %, preferably 2 to 80 weight% and, for example, 2 to 60 weight % of a matrix. According to one ormore embodiments, the catalyst comprises a dealuminated zeolite Y havingan overall atomic Si/AI ratio of more than 4, preferably between 8 and70, and preferably containing no extra-framework aluminous species. Saiddealuminated zeolite Y may be employed alone or in a mixture with abinder or a matrix, generally selected from the group consisting ofclays, aluminas, silica, magnesium, zirconia, titanium oxide, boronoxide, and any combination of at least two of these oxides, such assilica-alumina and silica-magnesium. Any of the known methods foragglomeration and shaping are applicable, such as, for example,extrusion, pelletization or droplet coagulation. Zeolites such as thedealuminated zeolites Y and their preparation are well known. Referencemay be made, for example, to U.S. Pat. No. 4,738,940.

According to one or more embodiments, the alkylating reactor is a fixedbed reactor.

According to one or more embodiments, the ethanol 30 is bio-based.According to one or more embodiments, the ethanol 30 comes from a sugarfermentation process. According to one or more embodiments, the ethanol30 comes from a sugar fermentation process in which the water content isbetween 0.5 weight % and 40 weight %.

According to one or more embodiments, the alkylation effluent 31 istransalkylated in the optional transalkylating section 14 to produce anethylbenzene-enriched fraction 32. According to one or more embodiments,the transalkylating reaction section 14 is fed with benzene, for examplewhen an excess of ethyl groups is observed in the alkylation effluent 31for producing ethylbenzene.

According to one or more embodiments, the ethylbenzene-enriched fraction32 is sent to the fractionating unit 15 to produce an ethylbenzenefraction 33, an aqueous fraction 34 comprising water and optionallyethanol, a benzene fraction 35, which may, for example, be at leastpartly recycled to the alkylating reaction section 13, optionally one ormore polyethylbenzene fractions 36 and 37, and optionally oligomersformed from the ethanol.

According to one or more embodiments, the ethylbenzene fraction 33 isfed to the isomerizing unit 11. In this way, all of the ethylbenzene,present initially in the feedstock and produced by alkylation in thealkylating reaction section 13, is introduced and converted intopara-xylene in the aromatic loop containing the isomerizing unit 11 andthe xylenes separating unit 10.

According to one or more embodiments, the alkylation effluent 31 is sentdirectly to the fractionating unit 15.

According to one or more embodiments, the fractionating unit 15comprises a series of fractionating columns (e.g., series of threecolumns) which is suitable for extracting the benzene fraction 35 (forexample at the top of the first fractionating column, the ethylbenzenefraction 33 (for example at the top of the second fractionating column),a first polyethylbenzene fraction 36 comprising diethylbenzene andoptionally triethylbenzene (for example at the top of the thirdfractionating column), and a second polyethylbenzene fraction 37comprising, in particular, tetraethylbenzene (for example at the bottomof the third fractionating column).

According to one or more embodiments, the first polyethylbenzenesfraction 36 is at least partly recycled to the transalkylating reactionsection 14. According to one or more embodiments, the firstpolyethylbenzenes fraction 36 is at least partly recycled to thetransalkylating unit 8. According to one or more embodiments, the secondpolyethylbenzenes fraction 37, called the tar fraction or heavyfraction, is withdrawn from the aromatic complex. According to one ormore embodiments, the second polyethylbenzenes fraction 37 is evacuatedwith the bottom fraction 26 from the heavy aromatics column 7.

In the transalkylating unit 8, the fraction 25 comprising C9-C10monoaromatics (and/or the hydrogenolysis effluent enriched inmethyl-substituted aromatic compounds, described hereinafter) is mixedwith the toluene-comprising fraction 23 coming from the top of thetoluene column 5, and is used to feed the reaction section of thetransalkylating unit 8, to produce xylenes by transalkylation ofaromatics with a deficit of methyl groups (toluene) and aromatics withan excess of methyl groups (e.g., tri- and tetramethylbenzenes).According to one or more embodiments, the transalkylating unit 8 is fedwith benzene (line not shown in FIG. 1), for example when an excess ofmethyl groups is observed, for the production of para-xylene.

According to one or more embodiments, the transalkylating unit 8comprises at least one first transalkylating reactor suitable for useunder at least one of the following operating conditions:

-   -   temperature of between 200° C. and 600° C., preferably of        between 350° C. and 550° C., and more preferably still of        between 380° C. and 500° C.;    -   pressure of between 2 and 10 MPa, preferably of between 2 and 6        MPa, and more preferably of between 2 and 4 MPa;    -   WWH of between 0.5 and 5 h⁻¹, preferably of between 1 and 4 h⁻¹,        and more preferably of between 2 and 3 h⁻¹.

According to one or more embodiments, the first transalkylating reactoris operated in the presence of a catalyst comprising zeolite, forexample ZSM-5. According to one or more embodiments, the secondtransalkylating reactor is a fixed bed reactor.

According to one or more embodiments, the transalkylating reactionsection 14 comprises at least one second transalkylating reactor whichis suitable for use under at least one of the following operatingconditions:

-   -   temperature of between 200° C. and 400° C., preferably of        between 220° C. and 350° C., and more preferably still of        between 250° C. and 310° C.;    -   pressure of between 1 and 6 MPa, preferably of between 2 and 5        MPa, and more preferably of between 3 and 5 MPa;    -   WWH of between 0.5 and 5 h⁻¹, preferably of between 0.5 and 4        h⁻¹, and more preferably of between 0.5 and 3 h⁻¹.

According to one or more embodiments, the second transalkylating reactoris operated in the presence of a catalyst comprising zeolite, forexample dealuminated zeolite Y (for example, a zeolite similar to thosedescribed in the alkylating catalyst part). According to one or moreembodiments, the second transalkylating reactor is a fixed bed reactor.

According to one or more embodiments, the effluents from the reactionsection of the transalkylating unit 8 are separated in a firstseparation column (not shown) downstream of said reaction section of thetransalkylating unit 8. A fraction 38 comprising at least some of thebenzene and the more volatile species (C6−) is extracted at the top ofthe first separating column and is sent to an optional stabilizingcolumn 12, enabling the removal in particular of the more volatilespecies (e.g., C5−) from the aromatic complex. The heavy fraction 21 ofthe effluents from the first separating column, comprising (e.g.,essentially) aromatics having at least 7 carbon atoms (A7+), isoptionally recycled to the fractionating train 4-7, for example to thebenzene column 4.

The fraction 24 comprising xylenes and ethylbenzene is treated in thexylenes separating unit 10 to produce a fraction or extract 39comprising para-xylene, and a raffinate 40. The extract 39 may besubsequently distilled (e.g., in the case of separation by adsorptionSMB), for example by means of an extract column and then a furthertoluene column (which are not shown), if toluene is used as a desorbent,in order to obtain high-purity para-xylene, which is exported as aprincipal product. The raffinate 40 from the xylenes separating unit 10comprises (e.g., essentially) ortho-xylene, meta-xylene andethylbenzene, and is used to feed the isomerizing unit 11.

According to one or more embodiments, the xylenes separating unit 10also separates a second toluene fraction 41, which comprises at least 90weight %, preferably at least 95 weight % and very preferably at least99 weight % of toluene. The toluene fraction 41 may be, for example, apart of the toluene which is used as a desorbent, when the xylenesseparating unit 10 comprises a simulated moving bed adsorption unit.According to one or more embodiments, the second toluene fraction 41 issent to the transalkylating unit 8.

In the isomerization reaction section (not shown) of the isomerizingunit 11, the isomers of para-xylene are isomerized, whereas theethylbenzene may be: isomerized to give a mixture of C8 aromatics, forexample if the aim is to produce primarily para-xylene; and/ordealkylated to produce benzene, for example if the aim is to produceboth paraxylene and benzene.

According to one or more embodiments, the effluents from theisomerization reaction section are sent to a second separation column(not shown) to produce, at the bottom, a para-xylene enrichedisomerizate 42, which is preferably recycled to the xylene column 6; andto produce, at the top, a hydrocarbon fraction 43 comprising compoundshaving 7 or fewer carbon atoms (C7−), which is sent to the optionalstabilizing column 12, for example with the fraction comprising at leastpart of the benzene, and the more volatile species 38.

According to one or more embodiments, the isomerizing unit 11 comprisesa first isomerization zone which works in liquid phase, and/or a secondisomerizing zone which works in gaseous phase, as is described in thepatents referenced earlier. According to one or more embodiments, theisomerizing unit 11 comprises a first isomerizing zone, which works inliquid phase, and a second isomerizing zone, which works in gaseousphase. According to one or more embodiments, a first part of theraffinate 40 is sent to the liquid-phase isomerizing unit, to give afirst isomerizate, which is used to feed, directly and at least partly,the separating unit 10; and a second part of the raffinate 40 is sent tothe gaseous-phase isomerizing unit, to give an isomerizate which is sentto the xylene column 6. According to one or more embodiments, theethylbenzene fraction 33 is sent on a majority basis (i.e., at least 50weight %, e.g., at least 60 weight %, preferably at least 70 weight %)into the first isomerizing zone, working in gaseous phase, to bepreferentially isomerized to para-xylene.

Advantageously, the isomerizing unit 11 enables the surplus ethylbenzeneprovided by the alkylating reaction section 13 to be converted with avery high selectivity.

According to one or more embodiments, the gaseous-phase isomerizing zoneis suitable for use under at least one of the following operatingconditions:

-   -   temperature greater than 300° C., preferably from 350° C. to        480° C.;    -   pressure of less than 4.0 MPa, and preferably from 0.5 to 2.0        MPa;    -   hourly space velocity less than 10 h⁻¹ (10 litres per litre per        hour), preferably between 0.5 h⁻¹ and 6 h⁻¹;    -   molar ratio of hydrogen to hydrocarbon of less than 10, and        preferably of between 3 and 6;    -   in the presence of a catalyst comprising at least one zeolite        having pores whose opening is defined by a ring of 10 or 12        oxygen atoms (10 MR or 12 MR), and at least one group VIII metal        with a content of between 0.1 and 0.3 weight % (reduced form),        endpoints included.

According to one or more embodiments, the liquid phase isomerizing zoneis suitable for use under at least one of the following operatingconditions:

-   -   temperature of less than 300° C., preferably 200° C. to 260° C.;    -   pressure of less than 4 MPa, preferably 2 to 3 MPa;    -   hourly space velocity (HSV) of less than 10 h⁻¹ (10 litres per        litre per hour), preferably between 2 and 4 h⁻¹;    -   in the presence of a catalyst comprising at least one zeolite        having pores whose opening is defined by a ring of 10 or 12        oxygen atoms (10 MR or 12 MR), preferably a catalyst comprising        at least one zeolite having pores whose opening is defined by a        ring of 10 oxygen atoms (10 MR), and more preferably a catalyst        comprising a ZSM-5 zeolite.

The term HSV corresponds to the hourly volume of hydrocarbon feedstockprojected, relative to the volume of catalyst charged.

According to one or more embodiments, the optional stabilizing column 12produces: at the bottom, a stabilized fraction 44 comprising (e.g.,essentially) benzene and toluene, which is optionally recycled to theentrance of the feedstock separating unit 1 and/or of the aromaticsextracting unit 3; and, at the top, a fraction 45 of more volatilespecies (e.g., C5−), which is removed from the aromatic complex.

According to one or more embodiments, the selective hydrogenolysing unit9 is suitable for:

-   -   treating the monoaromatics 25 having between 9 and 10 carbon        atoms; and    -   producing a hydrogenolysis effluent 46 enriched in        methyl-substituted aromatic compounds.

Specifically, the selective hydrogenolysing unit 9 may be suitable fortreating aromatics 25 having between 9 and 10 carbon atoms, byconverting one or more alkyl groups having at least two carbon atoms(ethyl, propyl, butyl, isopropyl groups, etc.) attached to a benzenering into one or more methyl groups, i.e., groups formed of a single CH₃group. The major advantage of the selective hydrogenolysing unit 9 isthat of increasing the CH₃ groups content and lowering the content ofethyl, propyl, butyl, isopropyl groups, etc., in the feedstock of theisomerizing unit 11, in order to increase the production rate ofxylenes, and especially of para-xylene, in said isomerizing unit 11.

According to one or more embodiments, the selective hydrogenolysing unit9 comprises at least one hydrogenolysis reactor which is suitable foruse under at least one of the following operating conditions:

-   -   temperature of between 300° C. and 550° C., preferably of        between 350° C. and 500° C., and more preferably still of        between 370° C. and 450°;    -   pressure of between 0.1 and 3 MPa, preferably of between 0.2 and        2 MPa, and more preferably of between 0.2 and 1 MPa;    -   molar H₂/HC (hydrocarbon feedstock) ratio of between 1 and 10,        and preferably of between 1.5 and 6;    -   WWH of between 0.1 and 50 h⁻¹ (e.g., 0.5-50 h⁻¹), preferably of        between 0.5 and 30 h⁻¹ (e.g., 1-30 h⁻¹), and more preferably of        between 1 and 20 h⁻¹ (e.g., 2-20 h⁻¹, 5-20 h⁻¹).

According to one or more embodiments, the hydrogenolysis reactor isoperated in the presence of a catalyst comprising at least one metalfrom group VIII of the Periodic Table, preferably nickel and/or cobalt,deposited on a porous support comprising at least one crystalline ornon-crystalline refractory oxide having or not having a structuredporosity. According to one or more embodiments, the metal from groupVIII is nickel. The presence of a promoter (group VIB VIIB VIII IB IIB)is also possible. The catalyst is supported on a refractory oxide (e.g.,alumina or silica), which has optionally been neutralized by treatmentwith a base.

According to one or more embodiments, the hydrogenolysis reactor is afixed bed reactor and the catalyst support takes the form of extra beds.According to one or more embodiments, the hydrogenolysis reactor is amoving bed reactor, and the catalyst support takes the form ofapproximately spherical beads. A moving bed may be defined as being agravity flow bed, such as those encountered in the catalytic reformingof gasolines.

FIG. 2 represents a schematic view of a process according to the presentinvention, enabling the production of para-xylene to be increased, wherethe transalkylating reaction section 14 is disposed downstream of thefractionating unit 15. According to one or more embodiments, thealkylation effluent 31 is separated in the fractionating unit 15 toproduce the ethylbenzene fraction 33, the aqueous fraction 34 comprisingwater and optionally ethanol, the benzene fraction 35, which may, forexample, be recycled at least partly to the alkylating reaction section13 and/or the transalkylating reaction section 14, optionally one ormore polyethylbenzene fractions 36 and 37, and optionally oligomersformed from the ethanol. The ethylbenzene fraction 33 is used to feedthe isomerizing unit 11.

Still referring to FIG. 2, according to one or more embodiments, atleast a portion of the first polyethylbenzenes fraction 36 is sent tothe transalkylating reaction section 14, to produce anethylbenzene-enriched fraction 47, which is returned to thefractionating unit 15. According to one or more embodiments, thetransalkylation zone 14 is at least partly fed with at least a portionof the benzene fraction 35 coming from the fractionating section 15.

The apparatus and the process for converting aromatic compounds asdescribed above comprise a transalkylating unit 8, which enablesconversion of the toluene and/or benzene into xylenes, usingmethylbenzenes. It is appreciated that the apparatus and the process forconverting aromatic compounds may comprise a disproportionation unit incombination with or in substitution of the transalkylating unit 8, withthe disproportionation unit allowing toluene to be converted intobenzene and xylene. For example, referring to FIG. 2, when adisproportionation unit 48 is used in place of the transalkylating unit8, the bottom effluent 29 from the xylene column 6 may be evacuated fromthe aromatic complex (omission of the heavy aromatics column 7 and theselective hydrogenolysis unit 9 which are present in FIG. 1).

According to one or more embodiments, the effluents from the reactionsection of the disproportionation unit 48 are separated in a thirdseparating column (not shown) downstream of said reaction section of thedisproportionation unit 48, to produce: a xylene-enriched fraction (50),which is preferably recycled to the isomerizing unit 11; and to producea benzene and toluene fraction 49, which is preferably sent to thebenzene column 4.

Referring to FIGS. 1 and 2, the apparatus and the process for convertingaromatic compounds as described above are suitable for sending the firsttoluene fraction 18 to the benzene column 4, and/or the toluene column5, and for sending the second toluene fraction 41 to the transalkylatingunit 8 or the disproportionation unit 48. It would be appreciated thatthe apparatus and the process for converting aromatic compounds may bemade suitable for sending the first toluene fraction 18 to thetransalkylating unit 8 or the disproportionation unit 48, and/or forsending second toluene fraction 41 to the benzene column 4, and/or thetoluene column 5.

The apparatus and the process according to the invention thereforeenable gains of up to 100% in terms of para-xylene to be obtained, whenthe entirety of the benzene is alkylated using the ethanol.

In the present specification, the groups of chemical elements are given,unless otherwise specified, according to the CAS classification (CRCHandbook of Chemistry and Physics, published by CRC Press, Editor inChief D. R. Lide, 81st edition, 2000-2001). For example, group VIIIaccording to the CAS classification corresponds to the metals fromcolumns 8, 9 and 10 according to the new IUPAC classification; group VIbaccording to the CAS classification corresponds to the metals fromcolumn 6 according to the new IUPAC classification.

Without further elaboration, it is believed that one skilled in the artcan, using the preceding description, utilize the present invention toits fullest extent. The preceding preferred specific embodiments are,therefore, to be construed as merely illustrative, and not limitative ofthe remainder of the disclosure in any way whatsoever.

In the foregoing and in the examples, all temperatures are set forthuncorrected in degrees Celsius and, all parts and percentages are byweight, unless otherwise indicated.

The entire disclosures of all applications, patents and publications,cited herein and of corresponding French application No. 19/14.582,filed Dec. 17, 2019, are incorporated by reference herein.

EXAMPLES Reference Apparatus Example

A reference apparatus example is used for converting a feedstockcomprising a mixture of aromatic compounds obtained from alignocellulosic biomass conversion process based on conversion bycatalytic pyrolysis.

The reference apparatus example is similar to the apparatus representedin FIG. 1, except that the transalkylating unit 8 is replaced with adisproportionation unit 48. Furthermore, the reference apparatus exampledoes not employ the following units:

-   -   heavy aromatics column 7;    -   selective hydrogenolysing unit 9;    -   stabilizing column 12;    -   alkylating reaction section 13;    -   transalkylating reaction section 14; and    -   fractionating unit 15.

The flow rates of said aromatic compounds of the feedstock to betreated, at the entrance of the reference apparatus, are as follows:

-   -   benzene: 2.63 t/h;    -   toluene: 5.64 t/h;    -   ethylbenzene: 0.15 t/h; and    -   xylenes: 3.56 t/h.

This gives a total of 11.98 t/h of aromatic compounds.

In the reference apparatus, the entirety of the toluene is convertedinto benzene and xylenes by a disproportionation unit. The xylenes inthe feedstock and produced by disproportionation are isomerized topara-xylene, which is separated from the xylenes mixture at thethermodynamic equilibrium at the exit of the isomerizing unit, by meansof a simulated moving bed adsorption unit. This collective of unitoperations allows production, in the best-case scenario (with atheoretical selectivity of 100% for each unit of operation) of thefollowing compounds:

-   -   benzene: 5.02 t/h;    -   para-xylene: 6.96 t/h    -   total aromatic: 11.98 t/h.

Inventive Apparatus Example

The inventive apparatus example allows both an increase in the totalamount of aromatics produced, for the same feedstock flow rate as in thereference apparatus, and production only of the compound of greateradded value: para-xylene.

The inventive apparatus example is similar to the apparatus representedin FIG. 1, except that the transalkylating unit 8 is replaced with adisproportionation unit 48. Furthermore, the inventive apparatus exampledoes not employ the following units:

-   -   heavy aromatics column 7;    -   selective hydrogenolysing unit 9; and    -   stabilizing column 12.

Particular additions relative to the reference apparatus scheme are thealkylating reaction section 13 and the transalkylating reaction section14, for alkylating the benzene with ethanol and for transalkylating thepolyethylbenzenes to ethylbenzenes. The product of the transalkylation14, namely the ethylbenzene, is introduced into the aromatic loop, whichcomprises the isomerizing unit 11, implemented with a liquid-phaseisomerization reaction and a gaseous-phase isomerization reaction, andthe xylenes separation unit 10.

According to the inventive apparatus example, and with the samefeedstock entering the complex and the same yields of the unitoperations as in the reference apparatus example, the performance data,by comparison with those for the reference apparatus, that are obtainedare shown in table 1.

TABLE 1 Reference apparatus Inventive apparatus example exampleFeedstock (t/h) — — EtOH 0 2.95 Benzene 2.63 2.63 Toluene 5.64 5.64Ethylbenzene: 0.15 0.15 Xylenes 3.56 3.56 Products (t/h) — — Benzene5.02 0 p-Xylene 6.96 13.78 Ethylbenzene: 0 0 H₂O [%] 0 1.15 Totalaromatics 11.98 13.78

Table 1 shows that the implementation according to the invention enablesproduction of 15 weight % of more aromatics (13.78 t/h rather than 11.98t/h) and the production only of para-xylene, with an increase inpara-xylene production of almost 100%.

The preceding examples can be repeated with similar success bysubstituting the generically or specifically described reactants and/oroperating conditions of this invention for those used in the precedingexamples.

From the foregoing description, one skilled in the art can easilyascertain the essential characteristics of this invention and, withoutdeparting from the spirit and scope thereof, can make various changesand modifications of the invention to adapt it to various usages andconditions.

The invention claimed is:
 1. A conversion apparatus for converting afeedstock (2) of aromatic compounds, comprising: a fractionating train(4-7) suitable for extracting at least one fraction comprising benzene(22), one fraction comprising toluene (23) and one fraction comprisingxylenes and ethylbenzene (24) from the feedstock (2); a xyleneseparating unit (10) suitable for treating the fraction comprisingxylenes and ethylbenzene (24) and for producing an extract (39)comprising para-xylene and a raffinate (40) comprising ortho-xylene,meta-xylene and ethylbenzene; an isomerizing unit (11) suitable fortreating the raffinate (40) and producing a para-xylene-enrichedisomerizate (42), which is sent to the fractionating train (4-7); and analkylating reaction section (13) suitable for treating at least part ofthe fraction comprising benzene (22) with an ethanol source (30) andproducing an alkylating effluent (31) comprising ethylbenzene, which issent to the isomerizing unit (11).
 2. The conversion apparatus accordingto claim 1, further comprising a transalkylating reaction section (14)suitable for transalkylating polyethylbenzenes present in the alkylationeffluent (31) and producing an ethylbenzene-enriched fraction (32; 47).3. The conversion apparatus according to claim 2, further comprising afractionating unit (15) suitable for treating the alkylation effluent(31) and producing a plurality of fractionation fractions comprising atleast one ethylbenzene fraction (33), which is sent to the isomerizingunit (11), one aqueous fraction (34) comprising water, and one benzenefraction (35).
 4. The conversion apparatus according to claim 3, whereinthe fractioning unit (15) is disposed downstream of the transalkylatingreaction section (14) and is suitable for treating theethylbenzene-enriched fraction (32; 47).
 5. The conversion apparatusaccording to claim 3, wherein the fractionating unit (15) is suitablefor producing additionally at least one polyethylbenzene fraction (36),and wherein the transalkylating reaction section (14) is disposeddownstream of the fractionating unit (15) and is suitable for treatingat least part of said polyethylbenzene fraction (36).
 6. The conversionapparatus according to claim 1, wherein the fractionated train (4-7) issuitable for extracting a C9-C10 monoaromatics fraction (25) from thefeedstock (2).
 7. The conversion apparatus according to claim 6, furthercomprising a transalkylating unit (8) suitable for treating the C9-C10monoaromatics fraction (25) with the fraction comprising toluene (23)and producing xylenes, which are sent to the fractionating train (4-7).8. The conversion apparatus according to claim 1, further comprising adisproportionating unit (48) suitable for treating the fractioncomprising toluene (23) and producing a xylene-enriched fraction (50),which is recycled to the isomerizing unit (11).
 9. A conversion processfor converting a feedstock (2) of aromatic compounds, comprising thefollowing steps: fractionating the feedstock in a fractionating train(4-7) to extract at least one fraction comprising benzene (22), onefraction comprising toluene (23) and one fraction comprising xylenes andethylbenzene (24); separating the fraction comprising xylenes andethylbenzene (24) in a xylene separating unit (10) and producing anextract (39) comprising para-xylene and a raffinate (40) comprisingortho-xylene, meta-xylene and ethylbenzene; isomerizing the raffinate(40) in an isomerizing unit (11) and producing a para-xylene-enrichedisomerizate (42); sending the para-xylene-enriched isomerizate (42) tothe fractionating train (4-7); alkylating at least part of the fractioncomprising benzene (22) with an ethanol source (30) in an alkylatingreaction section (13) and producing an alkylation effluent (31)comprising ethylbenzene; and sending the alkylation effluent (31)comprising ethylbenzene to the isomerizing unit (11).
 10. The conversionprocess according to claim 9, wherein the alkylating reaction section(13) comprises at least one alkylation reactor, which is used under thefollowing operating conditions: temperature of between 20° C. and 400°C.; pressure of between 1 and 10 MPa; molar benzene/ethanol ratio ofbetween 3 and 15; WWH of between 0.5 and 50 h⁻¹.
 11. The conversionprocess according to claim 10, wherein the alkylation reactor isoperated in the presence of a catalyst comprising a zeolite.
 12. Theconversion process according to claim 9, wherein the isomerizing unit(11) comprises a gas-phase isomerization zone and/or a liquid-phaseisomerization zone, wherein the gas-phase isomerization zone is usedunder the following operating conditions: temperature of greater than300° C.; pressure of less than 4.0 MPa; hourly space velocity of lessthan 10 h⁻¹; molar hydrogen-to-hydrocarbon ratio of less than 10; in thepresence of a catalyst comprising at least one zeolite having channelswhose opening is defined by a ring of 10 or 12 oxygen atoms, and atleast one group VIII metal in an amount of between 0.1 and 0.3 weight %,endpoints included, and wherein the liquid-phase isomerization zone isused under the following operating conditions: temperature of less than300° C.; pressure of less than 4 MPa; hourly space velocity of less than10 h⁻¹; in the presence of a catalyst comprising at least one zeolitehaving channels whose opening is defined by a ring of 10 or 12 oxygenatoms.
 13. The conversion process according to claim 9, furthercomprising the following step: transalkylating polyethylbenzenes presentin the alkylation effluent (31) in a transalkylating reaction section(14) and producing an ethylbenzene-enriched fraction (32; 47), andsending the ethylbenzene-enriched fraction (32; 47) to the isomerizingunit (11).
 14. The conversion process according to claim 13, wherein thetransalkylating reaction section (14) comprises at least onetransalkylation reactor, which is used under the following operatingconditions: temperature of between 200° C. and 400° C.; pressure ofbetween 1 and 6 MPa; WWH of between 0.5 and 5 h⁻¹.
 15. The conversionprocess according to claim 14, wherein the transalkylation reactor (14)is operated in the presence of a catalyst comprising a zeolite.
 16. Theconversion apparatus according to claim 1, further comprising afractionating unit (15) suitable for treating the alkylation effluent(31) and producing a plurality of fractionation fractions comprising atleast one ethylbenzene fraction (33), which is sent to the isomerizingunit (11), one aqueous fraction (34) comprising water, and one benzenefraction (35).
 17. The conversion apparatus according to claim 1,wherein the fractionating train comprises four columns including abenzene column (4) for producing the fraction comprising benzene (22), atoluene column (5) for producing the fraction comprising toluene (23), axylene column (6) for producing the fraction comprising xylenes andethylbenzene (24), and a heavy aromatic column (7) for producing aC9-C10 monoaromatics fraction (25); the xylene separating unit (10)comprises a crystallization unit or simulated moving bed unit; theisomerizing unit (11) comprises a gas-phase isomerization zone, aliquid-phase isomerization zone, or both a gas-phase isomerization zoneand a liquid-phase isomerization zone; and the alkylating reactionsection (13) comprises at least one alkylation reactor.
 18. Theconversion apparatus according to claim 17, wherein the isomerizing unit(11) comprises both a gas-phase isomerization zone and a liquid-phaseisomerization zone, wherein the gas-phase isomerization zone is usedunder the following operating conditions: temperature of greater than300° C., pressure of less than 4.0 MPa, hourly space velocity of lessthan 10 h⁻¹, molar hydrogen-to-hydrocarbon ratio of less than 10, and inthe presence of a catalyst comprising at least one zeolite havingchannels whose opening is defined by a ring of 10 or 12 oxygen atoms,and at least one group VIII metal in an amount of between 0.1 and 0.3weight %, endpoints included; and wherein the liquid-phase isomerizationzone is used under the following operating conditions: temperature ofless than 300° C., pressure of less than 4 MPa, hourly space velocity ofless than 10 h⁻¹, and in the presence of a catalyst comprising at leastone zeolite having channels whose opening is defined by a ring of 10 or12 oxygen atoms; and wherein said at least one alkylation reactor isused under the following operating conditions: temperature of between20° C. and 400° C., pressure of between 1 and 10 MPa, molarbenzene/ethanol ratio of between 3 and 15, and WWH of between 0.5 and 50h⁻¹.
 19. The conversion apparatus according to claim 18, wherein thegas-phase isomerization zone is used under the following operatingconditions: temperature from 350° C. to 480° C., pressure of from 0.5MPa to 2.0 MPa, hourly space velocity between 0.5 h⁻¹ and 6 h⁻¹, andmolar hydrogen-to-hydrocarbon ratio between 3 and 6; and wherein theliquid-phase isomerization zone is used under the following operatingconditions: temperature of 200° C. to 260° C., pressure of 2 to 3 MPa,hourly space velocity between 2 and 4 h⁻¹; and wherein said at least onealkylation reactor is used under the following operating conditions:temperature of between 150° C. and 400° C., pressure of between 2 and 7MPa, molar benzene/ethanol ratio of between 5 and 12, and WWH of between1 and 10 h⁻¹.